CN102849679A - Hydrogen-producing device and hydrogen-producing method thereof - Google Patents
Hydrogen-producing device and hydrogen-producing method thereof Download PDFInfo
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- CN102849679A CN102849679A CN201210111586XA CN201210111586A CN102849679A CN 102849679 A CN102849679 A CN 102849679A CN 201210111586X A CN201210111586X A CN 201210111586XA CN 201210111586 A CN201210111586 A CN 201210111586A CN 102849679 A CN102849679 A CN 102849679A
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Abstract
The invention discloses a hydrogen-producing device and a hydrogen-producing method thereof. The hydrogen-producing device comprises a liquid storage container, a main hydrogen-producing unit, and one or more minor hydrogen-producing units, wherein the minor hydrogen-producing unit is used as a heating unit of the main hydrogen-producing unit, the hydrogen or/and residual air produced by the minor hydrogen-producing unit is used as an initial start energy for the main hydrogen-producing unit, when the hydrogen or/and residual air produced by the minor hydrogen-producing unit reaches a set amount, the main hydrogen-producing unit is started, after that, the hydrogen or/and residual air produced by the main hydrogen-producing unit maintains the operation of the main hydrogen-producing unit. According to the invention, by adding the minor hydrogen-producing units to produce a certain amount of hydrogen, the produced hydrogen is burnt for being used as the starting heating source of the main hydrogen-producing unit; and the hydrogen produced by the main hydrogen-producing unit is used as the operation heating source of the main hydrogen-producing unit, thus the normal starting and operation of the device can be guaranteed with miniwatt motors, so that the miniaturization and mobility of the device can be guaranteed.
Description
Technical field
The invention belongs to technical field of hydrogen preparation, relate to a kind of hydrogen producer, relate in particular to a kind of hydrogen producer that needs low-power machine; Simultaneously, the invention still further relates to the hydrogen production process of above-mentioned hydrogen producer.
Background technology
In numerous new forms of energy, Hydrogen Energy will become the optimal energy of 21 century.This is because in the situation of coal, gasoline and hydrogen of burning identical weight, the energy that hydrogen produces is maximum, and the product of its burning is water, does not have lime-ash and waste gas, does not pollute the environment; Be carbonic acid gas and sulfurous gas and coal and oil combustion generate, can produce respectively Greenhouse effect and acid rain.Coal and reserves are limited, and hydrogen mainly is stored in the water, and unique product also is water after the burning, can produce continuously hydrogen, is finished never.
Hydrogen is a kind of colourless gas.Burning one gram Hydrogen Energy discharges your heat of 142 kilojoules, is 3 times of gasoline thermal value.The weight of hydrogen is light especially, and it has all gently been howed than gasoline, Sweet natural gas, kerosene, thereby carries, transports conveniently, is the only fuel of the vehicles that fly at a high speed such as space flight, aviation.Hydrogen can burn in oxygen, and the temperature of hydrogen flame can be up to 2500 ℃, thereby people's hydrogen cutting commonly used or weldable steel iron material.
In the Nature, the distribution of hydrogen is very extensive.Water is exactly large " warehouse " of hydrogen, wherein contains 11% hydrogen.There is 1.5% hydrogen the earth Rio; All contain hydrogen in the oil, coal, Sweet natural gas, animal and plant body etc.The main body of hydrogen is that the form with compound water exists, and earth surface about 70% is covered by water, and moisture storage capacity is very large, therefore can say that hydrogen is the energy of " inexhaustible, nexhaustible ".If can be with suitable method preparing hydrogen from water, hydrogen also will be the quite cheap energy of a kind of price so.
Having many uses of hydrogen, suitability is strong.It can not only be used as fuel, and metal hydride has the function that chemical energy, heat energy and mechanical energy are changed mutually.For example, hydrogen storage metal has the ability of inhaling the hydrogen heat release and absorbing heat and putting hydrogen, heat can be stored, and uses as heating and air-conditioning in the room.
Hydrogen at first is used on the automobile as geseous fuel.In May, 1976, the U.S. develops a kind of automobile of making fuel with hydrogen; Afterwards, Japan also succeeded in developing a kind of automobile take liquid hydrogen as fuel; In the latter stage seventies, the Mercedes of front Germany tests hydrogen, and they have only used five kg of hydrogen, has just made running car 110 kilometers.
As automobile fuel, not only clean with hydrogen, start easily at low temperatures, and little to the corrosive nature of engine, can prolong the work-ing life of engine.Because hydrogen can evenly mix with air, can save vaporizer used on the general automobile fully, thereby can simplify the structure of existing automobile.More interesting is to need only the hydrogen of adding 4% in gasoline.Use it as motor car engine fuel, but just fuel-economizing 40%, and need not petrol engine is done great improvement.
Hydrogen is easy to become liquid under certain pressure and temperature, thereby it is all very convenient with iron flask car, on-highway tractor or ship transportation.Liquid hydrogen both can be used as the fuel of automobile, aircraft, also can be used as the fuel of rocket, guided missile.The fly to Apollo Personnel investigation Program of the moon of the U.S. " Long March launch vehicle that number spaceship and China launch a man-made satellite., all make fuel with liquid hydrogen.
In addition, use hydrogen-hydrogen fuel cell directly to change into electric energy to Hydrogen Energy, make utilizing of Hydrogen Energy more convenient.At present, this fuel cell obtains using at spaceship and undersea boat, and effect is pretty good.Certainly, because cost is higher, also be difficult to generally use for the moment.
The annual production of hydrogen is about 3,600 ten thousand tons in the world now, and wherein the overwhelming majority is produced from oil, coal and Sweet natural gas, and this must consume original just mineral fuel very in short supply; The hydrogen that other has 4% is to produce with the method for brine electrolysis, but the electric energy that consumes is too many, does not calculate very much, and therefore, people are trying to explore to study the hydrogen manufacturing novel method.And can reduce the energy consumption in the Chemical Manufacture and reduce cost with methyl alcohol, water reformation hydrogen production, be expected to substitute the technique of " water electrolysis hydrogen production " that be called as electricity-eating tiger, utilize advanced methanol vapor reformation-pressure swing adsorption making pure hydrogen and be rich in CO
2Mixed gas, through further aftertreatment, can obtain simultaneously hydrogen and carbon dioxide gas.
Methyl alcohol and water vapour pass through catalyzer under certain temperature, pressure condition, under the effect of catalyzer, the transformationreation of methanol decomposition reaction and carbon monoxide occurs, generate hydrogen and carbonic acid gas, this is the gas solid catalytic reaction system of component more than, many reactions.Reactional equation is as follows:
CH
3OH→CO+2H
2 (1)
H
2O+CO→CO
2+H
2 (2)
CH
3OH+H
2O→CO
2+3H
2 (3)
The H that reforming reaction generates
2And CO
2, pass through again pressure swing adsorption process (PSA) or palladium membrane sepn with H
2And CO
2Separate, obtain high-purity hydrogen.The power consumption of pressure swing adsorption process is high, equipment is large, and is not suitable for small-scale hydrogen preparation.
In addition, existing hydrogen production equipment needs powerful motor in order to allow device start, and usually more than 3000KW (as shown in Figure 1), only motor just need to take a large amount of spaces, so that equipment can't miniaturization, movability is also very poor.
Summary of the invention
Technical problem to be solved by this invention is: a kind of hydrogen producer is provided, only needs low-power machine can guarantee the normal operation of equipment.
In addition, the present invention also provides the hydrogen production process of above-mentioned hydrogen producer, only needs low-power machine can guarantee the normal operation of equipment.
For solving the problems of the technologies described above, the present invention adopts following technical scheme:
A kind of hydrogen producer, described hydrogen producer comprise liquid container, main hydrogen producer, sub-hydrogen producer;
The hydrogen that described sub-hydrogen producer makes or/and residual air by burning as the initial start heating source of main hydrogen producer, the hydrogen that the group hydrogen producer makes is or/and residual air when satisfying set amount, starts main hydrogen producer; After this, the hydrogen partial that makes of main hydrogen producer is or/and residual air is kept main hydrogen producer operation by burning;
Described sub-hydrogen producer comprises: low-power machine, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber; Described liquid container, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber connect successively by pipeline;
Described low-power machine is in order to satisfy the environmental parameter of sub-vaporizer, sub-reformer chamber, sub-separate chamber; First alcohol and water in the liquid container is delivered to sub-reformer chamber reformation through processing, sub-separate chamber separates; With the hydrogen and the residual air burning that make, the element that need to heat for main hydrogen producer provides heat.
Described main hydrogen producer comprises: interchanger, vaporizer, reformer chamber, separate chamber; Described liquid container, interchanger, vaporizer, reformer chamber, separate chamber connect successively by pipeline;
First alcohol and water in the described liquid container is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange;
Methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °;
Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output;
Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus.
A kind of hydrogen producer, described hydrogen producer comprise liquid container, main hydrogen producer, one or more sub-hydrogen producer; Described sub-hydrogen producer is as the heating unit of main hydrogen producer;
The hydrogen that described sub-hydrogen producer makes or/and residual air as the initial start energy of main hydrogen producer, the hydrogen that the group hydrogen producer makes is or/and residual air when satisfying set amount, starts main hydrogen producer; After this, the hydrogen partial that makes of main hydrogen producer is or/and residual air is kept main hydrogen producer operation.
As a preferred embodiment of the present invention, described hydrogen producer comprises some sub-hydrogen producers, comprise the first sub-hydrogen producer, the second sub-hydrogen producer, the 3rd sub-hydrogen producer ..., the sub-hydrogen producer of N, each sub-hydrogen producer is connected successively; The hydrogen manufacturing amount of each sub-hydrogen producer unit time becomes large successively;
The first sub-hydrogen producer is as the heating unit of the second sub-hydrogen producer, and the sub-hydrogen producer of i is as the heating unit of i+1 hydrogen producer, and the sub-hydrogen producer of N is as the heating unit of main hydrogen producer; Wherein, i is integer, 1＜i＜N.
As a preferred embodiment of the present invention, described hydrogen producer comprises some sub-hydrogen producers, and the parton hydrogen producer is arranged in parallel.
As a preferred embodiment of the present invention, described sub-hydrogen producer comprises low-power machine, sub-reformer chamber, and described sub-reformer chamber is the small-scale reformer chamber, and the hydrogen manufacturing amount of sub-hydrogen producer unit time is less than the hydrogen manufacturing amount of main hydrogen producer time;
Described low-power machine is in order to satisfy the environmental parameter of sub-reformer chamber; First alcohol and water in the liquid container is delivered to sub-reformer chamber reformation through processing; With the hydrogen and the residual air burning that make, the element that need to heat for main hydrogen producer provides heat.
As a preferred embodiment of the present invention, described sub-hydrogen producer comprises: low-power machine, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber; Described liquid container, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber connect successively by pipeline;
Described low-power machine is in order to satisfy the environmental parameter of sub-vaporizer, sub-reformer chamber, sub-separate chamber; First alcohol and water in the liquid container is delivered to sub-reformer chamber reformation through processing, sub-separate chamber separates; With the hydrogen and the residual air burning that make, the element that need to heat for main hydrogen producer provides heat.
As a preferred embodiment of the present invention, described main hydrogen producer comprises: interchanger, vaporizer, reformer chamber, separate chamber; Described liquid container, interchanger, vaporizer, reformer chamber, separate chamber connect successively by pipeline;
First alcohol and water in the described liquid container is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange;
Methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °;
Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output;
Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus.
A kind of hydrogen production process of above-mentioned hydrogen producer, described method comprises the steps:
The promotor hydrogen producer prepares hydrogen, and the hydrogen that sub-hydrogen producer makes is or/and residual air, as the initial start energy of main hydrogen producer;
The hydrogen that the group hydrogen producer makes is or/and residual air when satisfying set amount, starts main hydrogen producer, and main hydrogen producer prepares hydrogen;
The hydrogen partial that main hydrogen producer makes is or/and residual air is kept main hydrogen producer operation.
As a preferred embodiment of the present invention, the hydrogen manufacturing step of described sub-hydrogen producer comprises:
Step S11: the first alcohol and water is delivered to sub-interchanger heat exchange by e Foerderanlage, enters sub-vaporizer gasification after the heat exchange;
Step S12: the methanol vapor after the gasification and water vapour enter sub-reformer chamber, and sub-reformer chamber is provided with catalyzer, and the temperature of sub-reformer chamber is 280 °-409 °;
Step S13: the Transfer pipe between sub-reformer chamber and the sub-separate chamber is through a sub-preheating temperature-controlling mechanism, and this sub-preheating temperature-controlling mechanism is in order to the gas of heating from sub-reformer chamber output; Described sub-preheating temperature-controlling mechanism is as the buffering between sub-reformer chamber and the sub-separate chamber, so that identical or approaching with the temperature of sub-separate chamber from the temperature of the gas of sub-reformer chamber output;
Step S14: the Temperature Setting in the described sub-separate chamber is 400 °-460 °; Be provided with sub-membrane separation apparatus in the sub-separate chamber, obtain hydrogen from the aerogenesis end of sub-membrane separation apparatus.
As a preferred embodiment of the present invention, the hydrogen manufacturing step of described main hydrogen producer comprises:
Step S21: the first alcohol and water is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange;
Step S22: methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °;
Step S23: the Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output;
Step S24: the Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus.
Beneficial effect of the present invention is: hydrogen producer and hydrogen production process thereof that the present invention proposes prepare certain hydrogen by increasing sub-hydrogen producer, with the startup heating source of this hydrogen partial (can also comprise residual air) burning as main hydrogen producer; The hydrogen that then makes by main hydrogen producer (can also comprise residual air) is as the operation heating source of main hydrogen producer.Therefore, hydrogen producer of the present invention only needs low-power machine (such as 30W) can guarantee the normal Start-up and operating performance of equipment, thereby can guarantee miniaturization and the movability of equipment.
Description of drawings
Fig. 1 forms synoptic diagram for the part of existing hydrogen producer.
Fig. 2 is that the part of hydrogen producer of the present invention forms synoptic diagram.
Fig. 3 is the startup schematic diagram of hydrogen producer of the present invention.
Fig. 4 is the startup schematic diagram of hydrogen producer of the present invention among the embodiment two.
Fig. 5 is the startup schematic diagram of hydrogen producer of the present invention among the embodiment three.
Embodiment
Describe the preferred embodiments of the present invention in detail below in conjunction with accompanying drawing.
Embodiment one
See also Fig. 2, the present invention has disclosed a kind of hydrogen producer, and described hydrogen producer comprises liquid container 10, main hydrogen producer 30, sub-hydrogen producer 20.
The hydrogen that described sub-hydrogen producer 20 makes or/and residual air by burning as the initial start heating source of main hydrogen producer 30, the hydrogen that group hydrogen producer 20 makes is or/and residual air when satisfying set amount, starts main hydrogen producer 30; After this, the hydrogen partial that makes of main hydrogen producer 30 is or/and residual air is kept main hydrogen producer operation by burning.
Described sub-hydrogen producer comprises: low-power machine, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber; Described liquid container, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber connect successively by pipeline.Described low-power machine is in order to satisfy the environmental parameter of sub-vaporizer, sub-reformer chamber, sub-separate chamber; As shown in Figure 3, low-power machine only needs 30W to satisfy the demand usually, can be with hydrogen and the residual air storage that makes, such as storage 5m
3First alcohol and water in the liquid container is delivered to sub-reformer chamber reformation after treatment, sub-separate chamber separates (also can not carry out lock out operation); With the hydrogen and the residual air burning that make, the element that need to heat for main hydrogen producer provides heat.
In the present embodiment, described main hydrogen producer comprises: interchanger, vaporizer, reformer chamber, separate chamber; Described liquid container, interchanger, vaporizer, reformer chamber, separate chamber connect successively by pipeline.First alcohol and water in the described liquid container is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange.Methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °.Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output.Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus.
More than introduced the composition of hydrogen producer of the present invention, the present invention also discloses a kind of hydrogen production process of above-mentioned hydrogen producer when disclosing aforesaid device.Described method comprises the steps: that the promotor hydrogen producer prepares hydrogen, and the hydrogen that sub-hydrogen producer makes is or/and residual air, as the initial start energy of main hydrogen producer.The hydrogen that the group hydrogen producer makes is or/and residual air when satisfying set amount, starts main hydrogen producer, and main hydrogen producer prepares hydrogen.The hydrogen partial that main hydrogen producer makes is or/and residual air is kept main hydrogen producer operation.
Wherein, the hydrogen manufacturing step of described sub-hydrogen producer comprises:
Step S11: the first alcohol and water is delivered to sub-interchanger heat exchange by e Foerderanlage, enters sub-vaporizer gasification after the heat exchange;
Step S12: the methanol vapor after the gasification and water vapour enter sub-reformer chamber, and sub-reformer chamber is provided with catalyzer, and the temperature of sub-reformer chamber is 280 °-409 °;
Step S13: the Transfer pipe between sub-reformer chamber and the sub-separate chamber is through a sub-preheating temperature-controlling mechanism, and this sub-preheating temperature-controlling mechanism is in order to the gas of heating from sub-reformer chamber output; Described sub-preheating temperature-controlling mechanism is as the buffering between sub-reformer chamber and the sub-separate chamber, so that identical or approaching with the temperature of sub-separate chamber from the temperature of the gas of sub-reformer chamber output;
Step S14: the Temperature Setting in the described sub-separate chamber is 400 °-460 °; Be provided with sub-membrane separation apparatus in the sub-separate chamber, obtain hydrogen from the aerogenesis end of sub-membrane separation apparatus.
The hydrogen manufacturing step of described main hydrogen producer comprises the steps:
Step S21: the first alcohol and water is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange;
Step S22: methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °;
Step S23: the Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output;
Step S24: the Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus.
Embodiment two
See also Fig. 4, in the present embodiment, described hydrogen producer comprises some sub-hydrogen producers, comprise the first sub-hydrogen producer, the second sub-hydrogen producer, the 3rd sub-hydrogen producer ..., the sub-hydrogen producer of N, each sub-hydrogen producer is connected successively; The hydrogen manufacturing amount of each sub-hydrogen producer unit time becomes large successively.
The first sub-hydrogen producer is as the heating unit of the second sub-hydrogen producer, and the sub-hydrogen producer of i is as the heating unit of i+1 hydrogen producer, and the sub-hydrogen producer of N is as the heating unit of main hydrogen producer; Wherein, i is integer, 1＜i＜N.
Embodiment three
See also Fig. 5, in the present embodiment, described hydrogen producer comprises some sub-hydrogen producers, and the parton hydrogen producer is arranged in parallel.
In sum, hydrogen producer and hydrogen production process thereof that the present invention proposes prepare certain hydrogen by increasing sub-hydrogen producer, with the startup heating source of this hydrogen partial (can also comprise residual air) burning as main hydrogen producer; The hydrogen that then makes by main hydrogen producer (can also comprise residual air) is as the operation heating source of main hydrogen producer.Therefore, hydrogen producer of the present invention only needs low-power machine (such as 30W) can guarantee the normal Start-up and operating performance of equipment, thereby can guarantee miniaturization and the movability of equipment.
Here description of the invention and application is illustrative, is not to want with scope restriction of the present invention in the above-described embodiments.Here the distortion of disclosed embodiment and change is possible, and the various parts of the replacement of embodiment and equivalence are known for those those of ordinary skill in the art.Those skilled in the art are noted that in the situation that does not break away from spirit of the present invention or essential characteristic, and the present invention can be with other form, structure, layout, ratio, and realize with other assembly, material and parts.In the situation that does not break away from the scope of the invention and spirit, can carry out other distortion and change to disclosed embodiment here.
Claims (10)
1. a hydrogen producer is characterized in that, described hydrogen producer comprises liquid container, main hydrogen producer, sub-hydrogen producer;
The hydrogen that described sub-hydrogen producer makes or/and residual air by burning as the initial start heating source of main hydrogen producer, the hydrogen that the group hydrogen producer makes is or/and residual air when satisfying set amount, starts main hydrogen producer; After this, the hydrogen partial that makes of main hydrogen producer is or/and residual air is kept main hydrogen producer operation by burning;
Described sub-hydrogen producer comprises: low-power machine, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber; Described liquid container, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber connect successively by pipeline;
Described low-power machine is in order to satisfy the environmental parameter of sub-vaporizer, sub-reformer chamber, sub-separate chamber; First alcohol and water in the liquid container is delivered to sub-reformer chamber reformation through processing, sub-separate chamber separates; With the hydrogen and the residual air burning that make, the element that need to heat for main hydrogen producer provides heat;
Described main hydrogen producer comprises: interchanger, vaporizer, reformer chamber, separate chamber; Described liquid container, interchanger, vaporizer, reformer chamber, separate chamber connect successively by pipeline;
First alcohol and water in the described liquid container is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange;
Methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °;
Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output;
Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus.
2. a hydrogen producer is characterized in that, described hydrogen producer comprises liquid container, main hydrogen producer, one or more sub-hydrogen producer; Described sub-hydrogen producer is as the heating unit of main hydrogen producer;
The hydrogen that described sub-hydrogen producer makes or/and residual air as the initial start energy of main hydrogen producer, the hydrogen partial that the group hydrogen producer makes is or/and residual air when satisfying set amount, starts main hydrogen producer; After this, the hydrogen that makes of main hydrogen producer is or/and residual air is kept main hydrogen producer operation.
3. hydrogen producer according to claim 2 is characterized in that:
Described hydrogen producer comprises some sub-hydrogen producers, comprise the first sub-hydrogen producer, the second sub-hydrogen producer, the 3rd sub-hydrogen producer ..., the sub-hydrogen producer of N, each sub-hydrogen producer is connected successively; The hydrogen manufacturing amount of each sub-hydrogen producer unit time becomes large successively;
The first sub-hydrogen producer is as the heating unit of the second sub-hydrogen producer, and the sub-hydrogen producer of i is as the heating unit of i+1 hydrogen producer, and the sub-hydrogen producer of N is as the heating unit of main hydrogen producer; Wherein, i is integer, 1＜i＜N.
4. it is characterized in that according to claim 2 or 3 described hydrogen producers:
Described hydrogen producer comprises some sub-hydrogen producers, and the parton hydrogen producer is arranged in parallel.
5. hydrogen producer according to claim 2 is characterized in that:
Described sub-hydrogen producer comprises low-power machine, sub-reformer chamber, and described sub-reformer chamber is the small-scale reformer chamber, and the hydrogen manufacturing amount of sub-hydrogen producer unit time is less than the hydrogen manufacturing amount of main hydrogen producer time;
Described low-power machine is in order to satisfy the environmental parameter of sub-reformer chamber; First alcohol and water in the liquid container is delivered to sub-reformer chamber reformation through processing; With the hydrogen and the residual air burning that make, the element that need to heat for main hydrogen producer provides heat.
6. hydrogen producer according to claim 2 is characterized in that:
Described sub-hydrogen producer comprises: low-power machine, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber; Described liquid container, sub-interchanger, sub-vaporizer, sub-reformer chamber, sub-separate chamber connect successively by pipeline;
Described low-power machine is in order to satisfy the environmental parameter of sub-vaporizer, sub-reformer chamber, sub-separate chamber; First alcohol and water in the liquid container is delivered to sub-reformer chamber reformation through processing, sub-separate chamber separates; With the hydrogen and the residual air burning that make, the element that need to heat for main hydrogen producer provides heat.
7. hydrogen producer according to claim 2 is characterized in that:
Described main hydrogen producer comprises: interchanger, vaporizer, reformer chamber, separate chamber; Described liquid container, interchanger, vaporizer, reformer chamber, separate chamber connect successively by pipeline;
First alcohol and water in the described liquid container is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange;
Methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °;
Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output;
Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus.
8. the hydrogen production process of the described hydrogen producer of claim 2 is characterized in that, described method comprises the steps:
The promotor hydrogen producer prepares hydrogen, and the hydrogen partial that sub-hydrogen producer makes is or/and residual air, as the initial start energy of main hydrogen producer;
The hydrogen that the group hydrogen producer makes is or/and residual air when satisfying set amount, starts main hydrogen producer, and main hydrogen producer prepares hydrogen;
The hydrogen partial that main hydrogen producer makes is or/and residual air is kept main hydrogen producer operation.
9. hydrogen production process according to claim 8 is characterized in that:
The hydrogen manufacturing step of described sub-hydrogen producer comprises:
Step S11: the first alcohol and water is delivered to sub-interchanger heat exchange by e Foerderanlage, enters sub-vaporizer gasification after the heat exchange;
Step S12: the methanol vapor after the gasification and water vapour enter sub-reformer chamber, and sub-reformer chamber is provided with catalyzer, and the temperature of sub-reformer chamber is 280 °-409 °;
Step S13: the Transfer pipe between sub-reformer chamber and the sub-separate chamber is through a sub-preheating temperature-controlling mechanism, and this sub-preheating temperature-controlling mechanism is in order to the gas of heating from sub-reformer chamber output; Described sub-preheating temperature-controlling mechanism is as the buffering between sub-reformer chamber and the sub-separate chamber, so that identical or approaching with the temperature of sub-separate chamber from the temperature of the gas of sub-reformer chamber output;
Step S14: the Temperature Setting in the described sub-separate chamber is 400 °-460 °; Be provided with sub-membrane separation apparatus in the sub-separate chamber, obtain hydrogen from the aerogenesis end of sub-membrane separation apparatus.
10. hydrogen production process according to claim 8 is characterized in that:
The hydrogen manufacturing step of described main hydrogen producer comprises:
Step S21: the first alcohol and water is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange;
Step S22: methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °;
Step S23: the Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output;
Step S24: the Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus.
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| CN112947658A (en) * | 2021-02-20 | 2021-06-11 | 华润智慧能源有限公司 | Control method, system and device of hydrogen production equipment |
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| CA2630168A1 (en) * | 2007-05-08 | 2008-11-08 | Air Products And Chemicals, Inc. | Hydrogen production method |
| CN101743190A (en) * | 2007-04-13 | 2010-06-16 | 能量转换科技公司 | Hydrogen system and method for starting up a hydrogen system |
| CN202575967U (en) * | 2012-04-16 | 2012-12-05 | 洁星环保科技投资（上海）有限公司 | Hydrogen-manufacturing device |
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| CN101743190A (en) * | 2007-04-13 | 2010-06-16 | 能量转换科技公司 | Hydrogen system and method for starting up a hydrogen system |
| CA2630168A1 (en) * | 2007-05-08 | 2008-11-08 | Air Products And Chemicals, Inc. | Hydrogen production method |
| CN202575967U (en) * | 2012-04-16 | 2012-12-05 | 洁星环保科技投资（上海）有限公司 | Hydrogen-manufacturing device |
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| CN105347300A (en) * | 2015-10-27 | 2016-02-24 | 北京氢璞创能科技有限公司 | Methanol to hydrogen machine system with rapid cold boot |
| CN105347300B (en) * | 2015-10-27 | 2018-05-15 | 北京氢璞创能科技有限公司 | A kind of quick cold start-up hydrogen from methyl alcohol machine system |
| CN112947658A (en) * | 2021-02-20 | 2021-06-11 | 华润智慧能源有限公司 | Control method, system and device of hydrogen production equipment |
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